Phase separation tank

ABSTRACT

A phase separation tank for separating an aqueous liquid from an organic liquid, the tank comprising:
         (A) A separation compartment having a sloped bottom wall and an aqueous liquid outlet;   (B) An organic liquid compartment separated from the separation compartment by an organic separator of a height that allows for the overflow of organic liquid from the separation compartment to the organic compartment;   (C) An aqueous liquid compartment separated from the organic liquid compartment by an aqueous separator and separated from the separation compartment by the organic compartment, the aqueous liquid compartment equipped with an aqueous liquid inlet; and   (D) Means for transferring aqueous liquid from the aqueous liquid outlet of the separation compartment to the aqueous liquid inlet of the aqueous compartment.

FIELD OF THE INVENTION

This invention relates to a process for the recovery of gold from anodeslimes. In one aspect the invention relates to a continuous, completelyhydrometallurgical process while in another aspect, the inventionrelates to a process employing improved mixing tank and phase separationtank designs.

BACKGROUND OF THE INVENTION

In the production of copper, copper-bearing ore is mined, concentrated,smelted and refined. The copper-bearing ore contains many otherelements, including many other metals, that must be separated from thecopper before the copper is ready for sale. Each step of the copperproducing process involves separating these other elements from thecopper until the copper reaches a desired sale purity, typically four“nines” purity, i.e., 99.99% copper.

The smelting stage of the copper producing process produces a copperanode which is typically three hundred plus pounds and 98+ percentcopper. These anodes contain, among other elements, various metals someof which are quite valuable. In order to separate these other elementsfrom the copper, these anodes are placed into a tank (or “electrolyticcell”) of electrolyte containing sulfuric acid and subjected to a directcurrent (DC). Under the influence of the electrolyte and electriccurrent, the copper anode dissolves and the copper plates onto astainless steel cathode to form a copper cathode of four nines purity.The other elements in the copper anode precipitate to the bottom of thetank and form “anode slimes”.

Among the components of the anode slimes are such valuable metals asgold and silver and over the years, much effort has been directed totheir recovery. These efforts have included both pyrometallurgical andhydrometallurgical methods each of which has its own advantages anddisadvantages.

One hydrometallurgical process of interest is that developed byKennecott Utah Copper and first described by J. E. Hoffmann et al. atthe 1995 International Conference of The Metallurgical Society of CIM,Hydrometallurgical Processing of Kennecott Refinery Slimes, COPPER95-COBRE 95 (Vol. III). In this process a slurry of the slimes and water(or an aqueous solution of hydrochloric acid) is formed, and the slurryis vigorously agitated with chlorine or hydrogen peroxide (a procedureknown as “wet chlorination”). The chlorinated (or liberated) gold isextracted from the resulting mixture in a multi-stage, countercurrentflow scheme in which dibutyl carbitol (DBC) is the extracting organicsolvent. The gold-loaded DBC is then scrubbed with an aqueous acid washto remove minor metal impurities, the gold reduced directly from theDBC, and recovered.

Variations on this theme have been developed over the years, e.g., U.S.Pat. No. 5,942,024, but the search for improvements continues. Forexample, a reduction in the footprint of the physical plant in which theprocess is conducted is desirable both from a capital and operating costperspective and from the amount of gold held in ‘inventory”. The largerthe physical plant, the costlier to build, operate and maintain theplant, and the more gold is held within the plant.

Another source for improvement is in the recovery of gold from theslimes. In the current process, some gold-loaded DBC is entrained in theaqueous phase of the extraction process, and this can result in a lossof 5 to 20 ppm gold in the raffinate. Any recovery of this “lost” goldcan result in a marked improvement to the overall economics of theprocess.

SUMMARY OF THE INVENTION

In one embodiment the invention is an apparatus for the recovery of goldfrom a gold-bearing filtrate, the apparatus comprising:

-   -   (A) A two-stage solvent extraction (S.E.) circuit comprising:        -   (1) A first S.E. mixing assembly;        -   (2) A first S.E. phase separation tank in fluid            communication with the first S.E. mixing assembly;        -   (3) A second S.E. mixing assembly in fluid communication            with the first S.E. phase separation tank; and        -   (4) A second S.E. phase separation tank in fluid            communication with the S.E. second mixing assembly; and    -   (B) A four-stage acid scrub (A.S.) circuit comprising:        -   (1) A first A.S. mixing assembly;        -   (2) A first A.S. phase separation tank in fluid            communication with the first A.S. mixing assembly;        -   (3) A second A.S. mixing assembly in fluid communication            with the first A.S. phase separation tank;        -   (4) A second A.S. phase separation tank in fluid            communication with the A.S. second mixing assembly;        -   (5) A third A.S. mixing assembly in fluid communication with            the second A.S. phase separation tank;        -   (6) A third A.S. phase separation tank in fluid            communication with the second A.S. mixing assembly;        -   (7) A fourth A.S. mixing assembly in fluid communication            with the third A.S. phase separation tank; and        -   (8) A fourth A.S. phase separation tank in fluid            communication with the fourth A.S. mixing assembly;            with the proviso that the second S.E. phase separation tank            is in fluid communication with the first A.S. mixing            assembly.

In one embodiment the invention is a process for the recovery of goldfrom an aqueous gold-bearing (Au-bearing) filtrate obtained from the wetchlorination of decopperized anode slimes, the process comprising thesteps of:

-   -   (A) Contacting the aqueous Au-bearing filtrate with dibutyl        carbitol (DBC) in a two-stage solvent extraction circuit to        remove the gold from the aqueous Au-bearing filtrate into the        DBC to form a gold-loaded DBC, the contacting performed in a        manner such that the aqueous Au-bearing filtrate is contacted in        the first stage of the solvent extraction circuit with DBC from        the second stage of the solvent extraction circuit and fresh DBC        is contacted in the second stage of the solvent extraction        circuit with the aqueous Au-bearing filtrate from the first        stage of the solvent extraction circuit; and    -   (B) Contacting the gold-loaded DBC from the second stage of the        solvent extraction circuit with an aqueous acid scrub of greater        than zero (>0) to 5 N hydrochloric acid in a four-stage acid        scrub circuit to remove impurities from the gold-loaded DBC into        the aqueous acid scrub to form an impurity-loaded aqueous scrub        solution and an impurity-depleted DBC; the contacting conducted        in a manner such that the gold-loaded DBC from the second stage        of the solvent extraction circuit is contacted in the first        stage of the aqueous acid scrub circuit with aqueous acid scrub        from the third stage of the aqueous acid scrub circuit, and the        gold-loaded DBC from the third stage of the aqueous acid scrub        is contacted with fresh aqueous acid scrub in the fourth stage        of the aqueous acid scrub circuit. In one embodiment the        gold-loaded DBC leaving the fourth stage of the aqueous acid        scrub circuit is contacted with a reducing agent to form        metallic gold.

In one embodiment the invention is a mixing assembly for intimatecontacting of an aqueous phase with an organic phase, e.g., an aqueousfiltrate comprising chlorinated gold and an organic phase comprisingDBC. In one embodiment the mixing assembly comprises:

-   -   (A) A vertical tank having a central vertical axis and        comprising a side wall, a bottom inlet and an upper outlet;    -   (B) A mixing device comprising:        -   (1) A shaft having a top end and a bottom end;        -   (2) A variable frequency drive (VFD) motor attached to or            near the top of the shaft in a manner to rotate the shaft            when the motor is activated;        -   (3) An axial flow impeller disposed on the shaft and beneath            the VFD motor;        -   (4) A radial flow plate disposed on the shaft and beneath            the axial flow impeller; and        -   (5) A radial flow impeller disposed on the shaft and beneath            the radial flow plate, the radial flow impeller not            extending beyond the radial flow plate;        -   the mixing device fitted into the tank and along the central            vertical axis of the tank such that the radial flow impeller            is located closest to the bottom inlet and the axial flow            impeller is located closest to the upper outlet;    -   (C) A baffle system attached to the side wall of the tank; and    -   (D) A liquid feed assembly connected to and in fluid        communication with the bottom inlet of the tank, the liquid feed        assembly comprising:        -   (1) A feed apparatus comprising top and bottom ends and a            divider extending from the top end to the bottom end to            divide the feed apparatus into first and second chambers,            the top end of each chamber in fluid communication with the            bottom inlet of the tank but neither chamber in fluid            communication with the other chamber;        -   (2) A first feed pipe connected to and in fluid            communication with the bottom end of the first chamber; and        -   (3) A second feed pipe connected to and in fluid            communication with the bottom end of the second chamber.            The mixing assembly of this embodiment of the invention is            not only useful in mixing the aqueous and organic phases of            this invention, but it is also useful in transferring the            organic/aqueous mixture from the first extraction stage to            the second extraction stage, from the second extraction            stage to the first settler stage, from the first settler            stage to the second settler stage, and so forth.

In one embodiment the invention is a phase separation tank forseparating an aqueous liquid from an organic liquid, the tank comprisinga sloped bottom wall. In one embodiment the phase separation tankcomprises:

-   -   (A) A separation compartment having a sloped bottom wall and an        aqueous liquid outlet;    -   (B) An organic liquid compartment separated from the separation        compartment by an organic separator of a height that allows for        the overflow of organic liquid from the separation compartment        to the organic compartment;    -   (C) An aqueous liquid compartment separated from the organic        liquid compartment by an aqueous separator and separated from        the separation compartment by the organic compartment, the        aqueous liquid compartment equipped with an aqueous liquid        inlet; and    -   (D) Means for transferring aqueous liquid from the aqueous        liquid outlet of the separation compartment to the aqueous        liquid inlet of the aqueous compartment.        The phase separation tank is useful in both the solvent        extraction and aqueous acid scrub circuits of this invention.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a schematic flow diagram of one embodiment of the goldrecovery process of this invention.

FIG. 2 is a side plane view of one embodiment of a mixing assembly ofthis invention.

FIG. 3 is a side plane view of one embodiment of a mixing device of thisinvention.

FIG. 4 is a side plane view of one embodiment of a liquid feed assemblyof this invention.

FIG. 5A is a side elevation of one embodiment of a phase separation tankof this invention.

FIG. 5B is a side plane view of the phase separation tank embodiment ofFIG. 5A.

FIG. 5C is a top plan view of the phase separation tank embodiment ofFIG. 5A.

Like numerals are employed to designate like parts through the drawingsand various items of equipment such as valves, fittings, pumps,condensers, holding tanks, feed tanks and the like are omitted so as tosimplify the description of the invention. However, those skilled in theart will recognize that such conventional equipment can be employed asdesired.

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENT Definitions

Unless stated to the contrary, implicit from the context, or customaryin the art, all parts and percentages are by weight. For purposes ofUnited States patent practice, the contents of any referenced patent,patent application or publication are incorporated by reference in theirentirety (or its equivalent U.S. version is so incorporated byreference) especially with respect to the disclosure of synthetictechniques, definitions (to the extent not inconsistent with anydefinitions specifically proved in this disclosure, and generalknowledge in the art.

The numerical ranges in this disclosure are approximate, and thus mayinclude values outside of the range unless otherwise indicated.Numerical ranges include all values from and including the lower and theupper values, in increments of one unit, provided that there is aseparation of at least two units between any lower value and any highervalue. As an example, if a compositional, physical or other property,such as, for example, molecular weight, viscosity, etc., is from 100 to1,000, it is intended that all individual values, such as 100, 101, 102,etc., and sub ranges, such as 100 to 144, 155 to 170, 197 to 200, etc.,are expressly enumerated. For ranges containing values which are lessthan one or containing fractional numbers greater than one (e.g., 1.1,1.5, etc.), one unit is considered to be 0.0001, 0.001, 0.01 or 0.1, asappropriate. For ranges containing single digit numbers less than ten(e.g., 1 to 5), one unit is typically considered to be 0.1. These areonly examples of what is specifically intended, and all possiblecombinations of numerical values between the lowest value and thehighest value enumerated, are to be considered to be expressly stated inthis disclosure. Numerical ranges are provided within this disclosurefor, among other things, aqueous/organic mixing ratios and componentconcentrations of various mixtures.

“Comprising”, “including”, “having” and like terms are not intended toexclude the presence of any additional component, step or procedure,whether or not the same is specifically disclosed. In order to avoid anydoubt, all processes claimed through use of the term “comprising” mayinclude one or more additional steps, pieces of equipment or componentparts, and/or materials unless stated to the contrary. In contrast, theterm, “consisting essentially of” excludes from the scope of anysucceeding recitation any other component, step or procedure, exceptingthose that are not essential to operability. The term “consisting of”excludes any component, step or procedure not specifically delineated orlisted. The term “or”, unless stated otherwise, refers to the listedmembers individually as well as in any combination.

“Fluid communication” and like terms mean that a fluid, i.e., a liquidor gas, can pass from one defined area to another defined area. Forexample and in the context of this invention, one extraction stage is influid communication with another extraction stage, or an extractionstage is in fluid communication with a scrub stage, or one scrub stageis in fluid communication with another scrub stage when the liquid,e.g., solution, emulsion or dispersion, can move from one to anotherunder the influence of either gravity or a pump.

Gold Recovery Process

The general process for the hydrometallurgical treatment of anode slimesis described by J. E. Hoffmann and K. E. Sutliff in their paper entitledHydrometallurgical Processing of Kennecott Refinery Slimes, ibid.Electrolytic refinery slimes, i.e., anode slimes, usually containbetween 10% and 40% elemental copper. Since copper can complicate thewet chlorination of the slimes, the slimes are typically first“de-copperized” by any conventional method, e.g., pressure oxidation,such that the final copper content of the slimes is reduced to less than0.5%. Pressure oxidation can also remove tellurium, if present, whichcan also complicate wet chlorination.

Upon completion of the pressure oxidation, the slimes are water washed,typically on a washing filter-press, to displace soluble copper from thefilter cake. The de-copperized slimes are then slurried in water or inan aqueous solution of hydrochloric acid (HCl) and subjected to vigorousstirring or other agitation. The metal components of the slimes areoxidized, typically with hydrogen peroxide (H₂O₂) in combination with achloride ion, typically provided as HCl. This wet chlorination isexothermic and thus generates heat which is removed. The chlorinatedslurry is filtered while hot, cooled and allowed to settle prior to asecond or polishing filtration. Solids collected during this polishingfiltration are recycled back to the chlorination reaction.

The filtrate from the polishing filtration is then subjected to atwo-stage extraction to recover the gold values. The first-stageextraction is conducted in a mixing assembly as first described aboveand more fully described below. In the first stage, the filtrate, anaqueous solution, is contacted with dibutyl carbitol (DBC), an organicextractant, in a countercurrent manner. DBC, also known as diethyleneglycol dibutyl ether, is a stable, low volatility, low toxicity solventwith an excellent selectivity for the gold species, e.g., 2HAuCl₄,carried within the aqueous filtrate. Extraction kinetics are fast andthus typically require a contact time of three minutes or less. Theacidity of the aqueous phase is typically maintained at greater than 0to 5 normal (N), preferably ≧1.5 to 3 N, HCl, and this represents anacceptable comprise between efficient chlorination and rejection ofimpurities during solvent extraction.

The first-stage aqueous and organic phases are gravity separated withina phase separation tank as first described above and more fullydescribed below. The phase separation typically takes about 30 minutes.The loaded DBC (e.g., 35-50 grams per liter (g/L)) is advanced toscrubbing and the first-stage raffinate is advance to the second-stageextraction in which it is contacted with the stripped or spent DBCreturning from gold reduction. The distribution coefficient of goldbetween the organic and aqueous phases varies, but two stages of solventextraction typically ensures a recovery of 99.9% of the aqueous goldcontent into the organic phase. The final gold content of the second andfinal raffinate typically does not exceed 1-5 parts per million (ppm).The second-stage extraction also is conducted in a mixing assembly asfirst described above and which is more fully described below, and thesecond-stage aqueous and organic phases are gravity separated as are thefirst-stage aqueous and organic phases, i.e., within a phase separationtank as first described above and more fully described below. Here too,the phase separation takes about 30 minutes.

The Au-loaded DBC phase may contain relatively small amounts of othermetals, e.g., selenium, tellurium, antimony, arsenic and bismuth, andthese are readily removed by an acid scrub comprising >0 to 5 N,preferably 1 to 4 N and more preferably 1.5 to 3 N, HCl. While this washcan be performed on a batch basis, in the practice of this invention itis continuous, countercurrent four-stage process. The scrubbers are themixing assemblies first described above and more fully described below,and the aqueous and organic phases are separated with phase separationtanks similar to that used to separate the phases after each stage ofthe solvent extraction circuit of this process.

After the fourth or last scrub stage, the Au-loaded DBC is contactedwith an aqueous solution of a reducing agent, e.g., oxalic acid and/orsodium oxalate. High acidity reduces the rate of reduction and as such,sodium oxalate is a preferred reducing agent. Reduction is performed atan elevated temperature, e.g., 75-80° C.

The reduction of the chlorinated gold species, e.g., HAuCl₄, produces acrystalline gold product which is readily filtered and washed free oforganic with hot water. Final traces of DBC are removed by an ethanolwash, and a Nutsch box filter is used for solids/liquids separation. Thegold-free DBC is returned to the solvent extraction circuit. Thereduction liquors which contain sodium chloride, hydrochloric acid andoxalic acid and gold are commingled with the DBC scrub liquors andreturned to the solvent extraction circuit.

FIG. 1 illustrates one embodiment of the invention. Anode slimes arede-copperized (not shown) and the de-copperized anode slimes are thensubjected to wet chlorination (not shown) to form an aqueous stream(filtrate) 13 comprising chlorinated gold. Organic DBC stream 11 is fedto first-stage solvent extractor 12 in which it is contacted with firstAu-depleted aqueous stream (raffinate) 13 a which is withdrawn fromaqueous phase collection area 14 a of second-stage phase separator 14.Organic DBC stream 11 further depletes the gold content of firstAu-depleted raffinate 13 a thus forming a second Au-depleted raffinate13 b and a first Au-loaded organic DBC stream 11 a. Au-depletedraffinate 13 b and first Au-loaded organic DBC stream 11 a are collectedin first-stage phase separation tank 15 in which first Au-loaded organicDBC stream 11 a and second Au-depleted raffinate 13 b are separated bygravity. Second Au-depleted raffinate 13 b is heavier or denser thanfirst Au-loaded organic DBC stream 11 a and as such, second Au-depletedraffinate 13 b collects at the bottom of phase separation tank 15 inaqueous phase collection area 15 b. Since first Au-loaded organic DBCstream 11 a is lighter or less dense than second Au-depleted raffinate13 b, first Au-loaded organic DBC stream 11 a collects in organic DBCcollection area 15 a which is on top of and in contact with secondAu-depleted raffinate 13 b.

Second Au-depleted raffinate 13 b is removed from organic DBC collectionarea 15 a to aqueous collection tank 16. First Au-loaded organic DBCstream 11 a is transferred to second stage solvent extractor 17 in whichit is contacted with Au-loaded aqueous stream 13 to form firstAu-depleted raffinate 13 a and second Au-loaded organic DBC stream 11 b.Au-depleted raffinate 13 a and second Au-loaded organic DBC stream 11 bare collected in second-stage phase separation tank 14 in which secondAu-loaded organic DBC stream 11 b and first Au-depleted raffinate 13 aare separated by gravity. First Au-depleted raffinate 13 a is heavier ordenser than second Au-loaded organic DBC stream 11 b and as such, firstAu-depleted raffinate 13 a collects at the bottom of second-stage phaseseparation tank 14 in aqueous phase collection area 14 a. Since secondAu-loaded organic DBC stream 11 b is lighter or less dense than firstAu-depleted raffinate 13 a, second Au-loaded organic DBC stream 11 bcollects in organic DBC collection area 14 b which is on top of and incontact with first Au-depleted raffinate 13 a.

Since the first or fresh charge of DBC solvent 11 to the solventextraction circuit is contacted first with an aqueous stream alreadydepleted of gold, i.e., first Au-depleted raffinate 13 a, the amount ofgold recovered from this first extraction stage is small relative to theamount of gold recovered from the second extraction stage, e.g., 1-5parts per million (ppm) versus 30-45 ppm. However, using a fresh chargeof DBC to contact the Au-depleted raffinate allows for a more efficientrecovery of the trace amounts of gold in the Au-depleted raffinate asopposed to contacting this stream with an Au-loaded DBC stream. Theamount of gold extracted into this fresh DBC charge is not enough tosignificantly lower its gold-extraction capacity upon contact with freshgold-bearing filtrate 13. This efficiency, coupled with the head-tailarrangement of the two stages, allows for a solvent extraction circuitfootprint to be smaller than a process in which each extraction stageuses a fresh charge of DBC solvent and/or each stage is operated on abatch basis.

Second Au-loaded organic DBC stream 11 b is transferred from organic DBCcollection area 14 b to first acid scrub vessel 18 in which secondAu-loaded organic DBC stream 11 b is contacted with aqueous acid scrub19 c to form third Au-loaded organic DBC stream 11 c (now partiallydepleted of impurities such as selenium, tellurium, bismuth, antimonyand arsenic) and impurities-loaded aqueous acid scrub 19 d. ThirdAu-loaded organic DBC stream 11 c and impurities-loaded aqueous acidscrub wash 19 d are collected in first-stage, acid scrub phaseseparation tank 20 in which third Au-loaded organic DBC stream 11 c andimpurities-loaded aqueous acid scrub 19 d are separated by gravity.Impurities-loaded aqueous acid scrub 19 d is heavier or denser thanthird Au-loaded organic DBC stream 11 c and as such, impurities-loadedaqueous acid scrub 19 d collects at the bottom of phase separation tank20 in aqueous phase collection area 20 b. Since third Au-loaded organicDBC stream 11 c is lighter or less dense than impurities-loaded aqueousacid scrub 19 d, third Au-loaded organic DBC stream 11 c collects inorganic DBC collection area 20 a which is on top of and in contact withimpurities-loaded aqueous acid scrub 19 d.

The acid scrub of the Au-loaded organic DBC stream that occurs in firstacid scrub vessel 18 and the subsequent phase separation of the aqueousand organic streams that occurs in first-stage, acid scrub phaseseparation tank 20, i.e., the first stage of the acid scrub circuit, isrepeated three times, once each in acid scrub vessels 21, 23 and 25 andacid scrub phase separation tanks 22, 24 and 26, respectively, i.e., thesecond, third and fourth stages of the acid scrub circuit. In each stagethe Au-loaded organic DBC stream (11 d, 11 e and 11 f) is contacted withthe impurities-loaded aqueous acid scrub wash (19 b, 19 a and 19), andin each stage the Au-loaded organic DBC stream is further depleted ofimpurities and the aqueous acid scrub wash is further loaded withimpurities. At the conclusion of the four stage aqueous acid scrub ofthe Au-loaded DBC organic stream, the impurities content, e.g., allmetals other than gold, of the Au-loaded organic DBC stream is reducedtypically to less than 40 ppm, more typically to less than 20 ppm andeven more typically to less than 5 ppm. The final Au-loaded organic DBCstream, i.e., stream 11 f, is removed from organic DBC collection area26 b at the bottom of phase separation tank 26 and transferred toAu-loaded organic DBC collection tank 27 from which it is eventuallytransferred downstream for gold reduction. The final aqueous acid scrub,i.e., stream 19 d, is removed from aqueous phase collection area 20 b atthe bottom of phase separation tank 20 to aqueous acid scrub collectiontank 16. This collected scrub or wash is treated to remove most, if notall, of the impurities that it has collected from the Au-loaded DBCorganic stream over the four acid scrub stages, and then transferredupstream for combination with the wet chlorination liquor prior to itsintroduction into the solvent extraction circuit. The aqueous acid scrubto organic DBC stream volume ratio is typically 1-1.5:1 over the courseof the four-stage circuit.

Since the first or fresh charge of aqueous acid scrub (stream 19) isintroduced into the acid scrub circuit at the fourth stage of thecircuit, its first contact is with Au-loaded DBC organic stream 11 ewhich has already has had its impurities content significantly reducethrough three prior countercurrent contacts with the aqueous acid scrubstream. This means that the acid scrub stream most able to extractimpurities from the Au-loaded DBC organic stream is employed to removesuch impurities from Au-loaded DBC organic stream most difficult fromwhich to remove such impurities, i.e., the Au-loaded DBC organic streamin which the non-gold metals are most dilute. This technique is carriedforward such that the Au-loaded DBC organic stream from which it iseasiest to extract impurities because their concentration is thegreatest is contacted with an acid scrub stream least capable ofextracting the impurities because its impurities content is thegreatest. The amount of impurities in the acid scrub stream that is usedin the first stage of the circuit is not enough to significantly lowerits impurities removal capacity. This efficiency, coupled with thehead-tail arrangement of the mixing assemblies and phase separationtanks, allows for the acid scrub circuit footprint to be smaller thanfor an acid scrub circuit in which each scrub stage uses a fresh chargeof acid wash and/or each stage is operated on a batch basis.

The combination of the small footprints from the solvent extraction andacid scrub circuits results is a smaller footprint for the overall goldrecovery process which, in turn, results in lower capital, operating andmaintenance costs to build, operate and maintain the circuits andoverall process. As illustrated in FIG. 1, these circuits are arrangedsuch that the mixing assembly is the head of a stage and the phaseseparation tank is the tail of the stage. The head and tail of eachstage of each of the solvent extraction and aqueous acid scrub circuitsare in close proximity to one another, and the stages are arranged suchthat the tail (i.e., phase separation tank) of one stage is in closeproximity to the head (i.e., the mixing assembly) of the adjacent stage.Moreover, the phase separation tank of the second stage of the solventextraction circuit is in close proximity of the mixing assembly of thefirst stage of the aqueous acid scrub circuit. This arrangementminimizes piping between the components of each stage, the stages ofeach circuit, and the circuits themselves. Less piping means a smalleroverall footprint for each stage and circuit, and this means lesscapital, operating and maintenance costs. Less piping also facilitates acontinuous operation of the individual circuits and the circuits intandem. This also means less gold held as “inventory” within theprocess. “In close proximity” means that the components of the stagesand circuits, and the circuits relative to one another, are spaced asclose to one another so as to minimize piping while maintainingsufficient separation (if any) to allow for ready access for operationaland maintenance purposes.

Mixing Assembly

FIG. 2 illustrates one embodiment of the mixing assembly of thisinvention. Mixing assembly 50 comprises vertical tank 51, mixing device52 fitted within vertical tank 50, baffle system 53 attached to the sidewall of vertical tank 51, and liquid feed assembly 54 connected to andin fluid communication with bottom inlet 55 (shown in FIG. 4) ofvertical tank 51. In one embodiment baffle system 53 comprises one ormore, preferably two, three or four, longitudinally interior baffleseach attached separately to the side wall of the tank and spaced aboutequally distance from one another. The baffles are flow-directing panelsthat impede the force or movement of liquids within the tank and assistin stabilizing the liquid flow within the tank, e.g., preventing orminimizing the formation of a vortex of the liquids due to the rotationof the impellers attached to the mixing device shaft. The baffles alsoassist in preventing or minimizing wobble or other motion of the tankresulting from the operation of the mixing device.

In one embodiment vertical tank 51 is equipped with false bottom 56which comprises bottom inlet 55 (shown in FIG. 4) and serves as adivider or separator between upper tank volume 57 in which the wetchlorination liquor and DBC organic solvent streams are mixed in thesolvent extraction circuit, or the Au-loaded DBC organic stream and acidscrub stream are mixed in the acid scrub circuit, and lower tank volume58 which is essentially empty other than for liquid feed assembly 54.Liquid feed assembly 54 is connect to and in fluid communication withorganic stream feed pipe 71 and aqueous stream feed pipe 70. Verticaltank 51 is also equipped with outlet 61 located at or near the top ofthe tank and above baffle system 53.

FIG. 3 illustrates one embodiment of mixing device 52. In thisembodiment, mixing device comprises shaft 62 having a top end 62 a and abottom end 62 b. Radial impeller 63 is disposed on shaft 62 near or atbottom end 62 b, radial flow extension plate 65 is disposed on shaft 62above radial impeller 63, and axial impeller 64 is disposed on shaft 62above radial flow extension plate 65. In one embodiment radial flowextension plate 65 is welded or otherwise affixed to radial impeller 63.In one embodiment the diameter of radial flow extension plate 65 is thesame or greater than the diameter of radial impeller 63 such that theouter edge of radial flow extension plate 65 is the same distance fromshaft 62 as is the outer edge of radial impeller 63 or the outer edge ofradial flow extension plate 65 extends beyond the outer edge of radialimpeller 63. In one embodiment axial impeller 64 is positioned on shaft62 at a point above radial flow extension plate 65 and below themidpoint of shaft 62, preferably closer to radial flow extension plate65 than the midpoint of shaft 62. Variable frequency drive (VFD) motor66 is attached to or near the top of shaft 62. Mixing device 52 isfitted into and along the central vertical axis of vertical tank 51 suchthat radial flow impeller 63 is located closest to and above bottominlet 55 of vertical tank 51, preferably no more than a few inches abovebottom inlet 55. The mixing device and several of its variations arefurther described in U.S. Pat. No. 5,511,881.

The impellers of the mixing device are rotated by the rotation of theshaft which in turn is rotated by the motor. The impellers impart aturbulent motion to the liquid contents of the tank as these contentsflow from the bottom of the tank to the top and out of the tank. Thismixing motion is not countercurrent inasmuch both the aqueous andorganic streams fed to the tank pass from the bottom of the tank to thetop of the tank and are brought into intimate contact with one anotherby the turbulent motion imparted from the rotation of the impellers. Theradial flow impeller also serves as a pump in the context that itimparts sufficient force and flow to the liquids to move them frombottom to top and out of the tank. The axial flow impeller primarilyserves to impart turbulence, and thus intimate mixing, to the aqueousand organic streams within the tank.

FIG. 4 illustrates one embodiment of the liquid feed assembly. In thisembodiment, liquid feed assembly 54 comprises liquid feed housing 67which comprises top end 67 a and bottom end 67 b. The shape of thehousing can vary to convenience, but typically its shape is cylindricalor tubular. Housing 67 is divided into two chambers of generally equalsize and configuration. The chambers are formed by divider 68 that runsthe length of housing 67 from top end 67 a to bottom end 67 b. Chamber69 a is separated from chamber 69 b by divider 68 such that neitherchamber is in fluid communication with the other chamber.

Chamber 69 a is in fluid communication with organic stream feed pipe 71and chamber 69 b is in fluid communication with aqueous feed pipe 70.Each chamber is also in fluid communication with volume 57 of verticaltank 51 such that the organic stream from organic stream pipe 71 passesthrough chamber 69 a and into tank 51 and the aqueous stream fromaqueous stream pipe 70 passes through chamber 69 b and into tank 51.Both the organic and aqueous streams enter tank 51 below radial impeller63 and do not commingle with one another until they have entered tank51. This separation of the organic and aqueous streams until they haveentered tank 51 allows for better volume control of each stream ascompared to configurations in which the streams are allowed to mix withone another, e.g. a configuration in which divider 68 does not run thefull length of housing 67 (see, for example, baffle B of FIG. 4 of U.S.Pat. No. 5,511,881). This is particularly important in that at somestages of the solvent extraction and/or aqueous acid scrub circuits thevolume ratio of organic to aqueous can be from 1:1 to 8:1 to 20:1 ormore, particularly in the solvent extraction circuit and if thesestreams are allowed to bleed into one another prior to entering tank 51,then maintaining these volume ratios can be very difficult, if notimpossible.

Mixing assembly 50 operates in a manner that allows for a fast, thoroughmixing of organic and aqueous phases such that in the solvent extractioncircuit gold is transferred from the wet chlorination liquor to the DBCorganic solvent phase, and in the acid scrub wash circuit impurities aretransferred from the Au-loaded DBC organic phase to the acid scrubstream in a quantitative manner. In the solvent extraction circuit, wetchlorination liquor passes from aqueous feed pipe 70, into and throughchamber 69 a, through inlet 55, and into tank 51. DBC passes fromorganic feed pipe 71, into and through chamber 69 b, through inlet 55,and into tank 51. Once in tank 51, the dual impeller system pumps andmixes the two streams to create an intense turbulence insuring thoroughcontact of the two streams that in turn allows for a quantitativeextraction of gold from the wet chlorination liquor into the DBC. Theaction of the impellers not only mix the two streams, but also lifts thestreams from the bottom of tank 51 to the top of tank 51 such that theblended streams can discharge on a continuous basis through outlet 61into a phase separation tank. Baffle system 53, e.g., four flat sheetsof metal, glass or other like material protruding from the tank sidewallinto the tank volume 57 (typically protruding only a few inches into thetank volume 57) insures that a vortex is not formed which would impair athorough mixing of the streams. The impellers are affixed to the shaftsuch that the rotation of the shaft the VFD motor necessarily rotatesthe impellers. This mixing device and tank configuration allowsextraction to occur with incoming liquid streams of different physicalproperties at controlled flow rates optimized for gold extraction.

The operation of the tank and mixing device to remove impurities from anAu-loaded DBC organic stream by contact with an aqueous acid scrub isessentially the same as for the solvent extraction circuit with theunderstanding that the flow rates of the organic and aqueous streams andthe impeller speeds typically differ. Optimization of the solventextraction and acid scrub circuits is well within the skill of theordinary artisan.

Phase Separation Tank

FIGS. 5A-C illustrate one embodiment of a phase separation tank of thisinvention. Phase separation tank 72 can have any general configurationas long as bottom 73 (i.e., the bottom wall beneath phase separationzone or compartment 80) is sloped. Sloped bottom 73 can extend for thelength of the separation compartment, or it can flatten out as shown bybottom segment 74. The inclination of the slope is typically 10 to 60degrees, more typically 10 to 20 degrees and even more typically 10 to15 degrees, off horizontal plane 75 (here the plane in which the bottomwalls of organic liquid compartment 81 and aqueous liquid compartment 83lie). Tank 72 is equipped with a feed inlet 76, organic separator 77 andaqueous separator 78. Front wall 79 of tank 72 and organic separator 77form separation zone 80, organic separator 77 and aqueous separator 78form organic compartment 81, and aqueous separator 78 and back wall 82of tank 72 form aqueous compartment 83. Drain 84 is located on thebottom wall of separation zone 80, typically on flattened segment 74 butif separation zone 80 is without flattened segment 74, then at thelowest or near lowest point on sloped bottom 73. Of course, the side andbottom walls of tank 72 complete phase separation zone 80, organiccompartment 81 and aqueous compartment 83. The bottom wall of tank 72under the organic and aqueous compartments is typically flat, elevatedrelative to the lowest point on the sloped bottom wall or flattenedsegment, and form horizontal plane 75 against which the inclination ofsloped wall 73 is measured.

Organic compartment 81 is equipped with outlet 87 which is connected topipe 88 for discharge of the organic phase from organic compartment 81.Separation zone 80 is equipped with aqueous phase outlet 85 which is influid communication with aqueous compartment 83 by pipe 86 a, inlet 86 band standpipe 86 c. Aqueous compartment 83 is also equipped withstandpipe 89 (FIG. 5C) which is in fluid communication with an outletand a drain pipe (neither shown) for removing excess aqueous phase fromaqueous compartment 83.

In operation a mixture of organic and aqueous streams is fed to thephase separation tank from a solvent extraction vessel or an acid scrubwash vessel. The streams enter the phase separation tank through inlet76 in a blended state. Once inside phase separation zone 80, the streamsare allowed to gravity separate due to their density differences withthe aqueous stream partitioning toward the bottom of the tank and theorganic stream partitioning toward the top of the tank. The phaseseparation is assisted by the sloped bottom of the tank because theaqueous phase droplets will move down the slope as they contact it andthen coalesce with one another as they collect in the bottom of thetank. This phase separation tank design facilitates a faster and/or morecomplete separation of the organic and aqueous phases than does a tankin which the bottom wall is without a slope, particularly without aslope of at least 10°.

The height of organic separator 77 is lower than the height of the tanksidewalls and as such, the partitioned organic phase overflows fromseparation zone 80 into organic compartment 81. The separated organicphase is then drained from organic compartment 81 through outlet 87 andpipe 88 for further processing, aqueous acid scrub if from the secondphase separation tank of the solvent extraction circuit or goldreduction if from the fourth phase separation tank of the aqueous acidscrub circuit.

The partitioned aqueous phase is removed from separation zone 80 throughoutlet 85 and transferred to aqueous compartment 83 by pipe 86 a, inlet86 b and standpipe 86 c. Aqueous compartment 83 is used to maintain thedesired liquid level within separation zone 80 and as the liquid levelneeds to be lowered for whatever reason, partitioned aqueous phase istransferred from separation zone 80 to aqueous compartment 83. If thelevel of the aqueous phase in aqueous compartment 83 becomes too high,then the level of the aqueous phase is lowered by removing the aqueousphase through standpipe 89 and an outlet and drain pipe not shown. Theaqueous phase enters standpipe 89 by overflow, i.e., as the level of theaqueous phase in aqueous compartment 83 rises above the top of standpipe89, it enters into standpipe 89. The discharged aqueous phase iscollected, treated and recycled and/or discharged from the gold recoveryprocess.

It is specifically intended that the present invention not be limited tothe embodiments and illustrations contained herein, but include modifiedforms of those embodiments including portions of the embodiments andcombinations of elements of different embodiments as come within thescope of the following claims.

We claim:
 1. A phase separation tank for separating an aqueous liquidfrom an organic liquid, the tank comprising: (A) A separationcompartment having a sloped bottom wall and an aqueous liquid outlet;(B) An organic liquid compartment separated from the separationcompartment by an organic separator of a height that allows for theoverflow of organic liquid from the separation compartment to theorganic compartment; (C) An aqueous liquid compartment separated fromthe organic liquid compartment by an aqueous separator and separatedfrom the separation compartment by the organic compartment, the aqueousliquid compartment in fluid communication with the separationcompartment and equipped with an aqueous liquid inlet standpipe and anaqueous liquid outlet standpipe; and (D) Means for transferring aqueousliquid from the aqueous liquid outlet of the separation compartment tothe aqueous liquid inlet of the aqueous compartment.
 2. The phaseseparation tank of claim 1 in which the inclination of the slope of thebottom wall of the separation compartment is between 10° and 60°.